Film ozonolysis in a tubular or multitubular reactor

ABSTRACT

The disclosure relates to a method of performing ozonolysis or ozone-based oxidation on a liquid or emulsified reagent using a tubular falling firm reactor with one or multiple tubes wherein the combined ozone and carrier gas flow is co-current.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of U.S. application Ser. No. 15/320,250, filed on Dec. 19, 2016, which is a National Stage Entry under 35 U.S.C. § 371 of International Application No. PCT/US15/36589, filed Jun. 19, 2015, which claims priority to U.S. Provisional Application No. 62/015,311, filed Jun. 20, 2014, and U.S. Provisional Application No. 62/163,022, filed May 18, 2015, each of which are incorporated herein by reference in their entireties.

BACKGROUND

Ozonolysis or ozone-based oxidation of reagents currently in use in the chemical industry generally rely on processing large amounts of material in either tray-type continuous ozonation systems or in batch systems, e.g., U.S. Pat. No. 2,813,113. The use of either type of established method, however, results in the accumulation of peroxide intermediates that can be unstable and present a significant explosion risk. Alternatively, processing small amounts of material in a continuous fashion can significantly reduce these risks. Solutions to address this important safety issue include the use of microstructured falling film reactors such as those described in U.S. Pat. No. 7,825,277 B2, and available from ThalesNano, Inc. These technologies, however, have not been adapted for use in large-scale (multi-ton) manufacturing processes, owing to challenges with throughput and the operation costs associated with maintaining large numbers of reaction vessel channels and precisely calibrated instruments.

Other commercial reaction technologies use sparging or aeration techniques to drive interactions between liquid and gaseous reagents, which can introduce local hot spots and requires that the gaseous reagent be present at high pressures. The disclosure described herein addresses the need for a method of industrial-scale ozonolysis that is safer and more efficient than conventional methods.

SUMMARY OF THE DISCLSOURE

The approach to ozonolysis described herein functions using gravity assisted co-current reagent flow to facilitate gaseous reagent diffusion into a liquid or emulsified reagent, which simplifies the reaction setup and minimizes the mechanical energy required, all while achieving a scalable and continuous process that does not allow for the accumulation of large amounts of hazardous intermediates, thus rendering the process and equipment described herein suitable for large, industrial-scale ozonolysis.

In one embodiment of the current disclosure a monotubular or multitubular reactor is used for ozonolysis or ozone-based oxidation in which:

-   -   (a) homogeneity of the reagent-containing film and thermal         exchange is maximized,     -   (b) selection of the optimum size of the individual tubes is         based on the best compromise between maximum internal diameter         (for optimum throughput) and minimum height (for reduced head         loss) while maintaining mechanical simplicity (for reduced         maintenance), and     -   (c) distribution of the gaseous ozone-containing reagent with         negligible head loss is conditioned by the reagent-containing         film thickness and corresponding flow rate such that the         conversion and temperature profiles are optimized along the tube         length.

The parameters above can be optimized both theoretically and empirically, and can be used to ensure excellent results without the need for calibration when changing the flow rate and/or composition of the liquid or emulsified reagent.

In some embodiments, the method of performing ozonolysis or ozone-based oxidation on a liquid or emulsified reagent entails using a tubular falling film reactor with one or multiple tubes wherein the combined ozone and carrier gas flow is co-current.

In some embodiments, the diameter of the tube(s) is between 5 mm and 5 m.

In some embodiments, the diameter of the tube(s) is between 5 mm and 50 mm.

In some embodiments, the diameter of the tube(s) is between 5 mm and 30 mm.

In some embodiments, the diameter of the tube(s) is between 10 mm and 25 mm.

In some embodiments, the diameter of the tube(s) is 25 mm.

In some embodiments, the diameter of the tube(s) is 10 mm.

In some embodiments, the diameter of the tube is between 50 mm and 5 m.

In some embodiments, the diameter of the tube is between 0.5 m and 5 m.

In some embodiments, the diameter of the tube is between 50 mm and 5 m and an annular element is added to the center of the tube to regulate gas flow and to add additional film surface area.

In some embodiments, the length of the tube(s) is between 1 and 20 m.

In some embodiments, the length of the tube(s) is between 1 and 7 m.

In some embodiments, the length of the tube(s) is 1.7 m.

In some embodiments, the length of the tube(s) is 6 m.

In some embodiments, the length of the tube(s) is between 7 and 20 m.

In some embodiments, the distribution of gas within the tube(s) may be controlled by annular spaces for gas flow within the tube(s).

In some embodiments, multiple falling film tube reactors are used in series to process a continuous stream of liquid or emulsified reagent.

In some embodiments, the method of performing ozonolysis or ozone-based oxidation on a liquid or emulsified reagent with a gaseous reagent (e.g., comprising ozone and one or more carrier gases) includes:

-   -   (a) feeding the liquid or emulsified reagent from a common         liquid or emulsified reagent feeding chamber that is maintained         completely full through annular slots and into a plurality of         parallel and substantially identical tubes, as to form a liquid         or emulsified reagent film on the internal surface of each tube;     -   (b) feeding the gaseous reagent through the annular slots and         into the tubes from a gaseous reagent feeding chamber, the         feeding pressure of the gaseous reagent being substantially the         same as the pressure loss from the gaseous reagent flow through         the tubes containing the liquid or emulsified reagent film, but         less than the feeding pressure of the liquid reagent;     -   (c) cooling the tubes by flowing a liquid coolant through a         housing surrounding the tubes; and     -   (d) collecting reaction product(s) and gaseous reagent exhaust         in one or more product containers connected to the end of the         tubes opposite that connected to the annular slots.

In some embodiments, the length of the tubes used in this method is between 1 and 20 m.

In some embodiments, the length of the tubes used in this method is between 1 and 7 m.

In some embodiments, the length of the tubes used in this method is 1.7 m.

In some embodiments, the length of the tubes used in this method is 6 m.

In some embodiments, the length of the tubes used in this method is between 7 and 20 m.

In some embodiments, the internal diameter of the tubes used in this method is between 5 mm and 5 m.

In some embodiments, the internal diameter of the tubes used in this method is between 5 mm and 50 mm.

In some embodiments, the internal diameter of the tubes used in this method is between 5 mm and 30 mm.

In some embodiments, the internal diameter of the tubes used in this method is between 10 mm and 25 mm.

In some embodiments, the internal diameter of the tubes used in this method is 25 mm.

In some embodiments, the internal diameter of the tubes used in this method is 10 mm.

In some embodiments, the internal diameter of the tubes used in this method is between 50 mm and 5 m.

In some embodiments, the internal diameter of the tubes used in this method is between 0.5 m and 5 m.

In some embodiments, the feeding pressure of the gaseous reagent used in this method is between 0.1 and 5 bar.

In some embodiments, the feeding pressure of the gaseous reagent used in this method is between 0.1 and 0.5 bar.

In some embodiments, the feeding pressure of the gaseous reagent used in this method is between 0.2 and 0.4 bar.

In some embodiments, the feeding overpressure of the liquid or emulsified reagent with respect to the feeding pressure of the gaseous reagent is between 5 and 15 cm of liquid column.

In some embodiments, the carrier gas contains, at least in part, gaseous reagent exhaust from one or more product containers.

In some embodiments, the reagent is a liquid.

In some embodiments, the reagent is an emulsion in water.

In some embodiments, the liquid or emulsified reagent or reagent mixture is the starting material which is reacted with ozone to yield oxidized product(s).

In some embodiments, the starting material is an alkene, alkyne, or any other compound that may be oxidized with ozone.

In some embodiments, the liquid or emulsified reagent comprises hydroxycitronellene, methoxycitronellene, rose ketones (e.g., Ionone), fatty acid methyl esters (FAME), triglycerides, fatty acids, fatty alcohols, fatty esters, diterpenes, sesquiterpenes, monoterpenes, allyl ethers, alpha olefins, rosin acids, tertiary amines, alkanes, amides, carboxylic acids, or compounds containing an aromatic ring.

In some embodiments, the reagent introduced into the reactor is any compound that is susceptible to ozone oxidation. In some embodiments, the reagent comprises any alkane, amide, carboxylic acid, or aromatic ring.

In some embodiments, the reaction products may be further reduced or oxidized to generate corresponding carbonyls, alcohols, and/or acids.

In some embodiments, the liquid or emulsified reagent comprises hydroxycitronellene.

In some embodiments, the liquid or emulsified reagent is a hydroxycitronellene emulsion in water.

In some embodiments, the liquid or emulsified reagent is a hydroxycitronellene solution in methanol.

In some embodiments, the product of the method described herein is hydroxymelonal.

In some embodiments, the liquid or emulsified reagent comprises methoxycitronellene.

In some embodiments, the liquid or emulsified reagent is a methoxycitronellene emulsion in water.

In some embodiments, the liquid or emulsified reagent is a methoxycitronellene solution in methanol.

In some embodiments, the product is methoxymelonal.

In some embodiments, the liquid or emulsified reagent comprises fatty acid methyl esters (FAME).

In some embodiments, the liquid or emulsified reagent is a FAME emulsion in water.

In some embodiments, the liquid or emulsified reagent is a FAME solution in methanol.

In some embodiments, the product produced by the method described herein comprises methyl azealdehyde and nonanal.

In some embodiments, the liquid or emulsified reagent comprises an unsaturated olechemical such as a triglyceride, a fatty acid, a fatty alcohol, or a fatty acid ester.

In some embodiments, the liquid or emulsified reagent comprises a diterpene such as abietic acid or its ester.

In some embodiments, the liquid or emulsified reagent comprises a mono- or di-unsaturated sesquiterpene.

In some embodiments, the liquid or emulsified reagent comprises a mono- or di-unsaturated monoterpene or terpene derivative such as pinene or limonene.

In some embodiments, the liquid or emulsified reagent comprises an allyl ether of 10 to 30 carbon atoms.

In some embodiments, the liquid or emulsified reagent comprises an alpha olefin of 10 to 30 carbon atoms.

In some embodiments, the liquid or emulsified reagent comprises a rose ketone. In some embodiments the rose ketone is Ionone.

In some embodiments, the product of the method described herein is cyclocitral.

In some embodiments, the liquid or emulsified reagent comprises a tertiary amine.

In some embodiments, the product of the method described herein is an N-oxide derivative.

In some embodiments, the carrier gas is O₂.

In some embodiments, the carrier gas is a mixture of O₂ and N₂. In some embodiments, the carrier gas is about 95% O₂ and 5% about N₂, about 90% O₂ and about 10% N₂, about 85% O₂ and about 15% N₂, about 80% O₂ and about 20% N₂, about 70% O₂ and about 30% N₂, about 60% O₂ and about 40% N₂, about 50% O₂ and about 50% N₂, about 40% O₂ and about 60% N₂, about 30% O₂ and about 70% N₂, about 20% O₂ and 80% N₂, or 10% O₂ and 90% N₂, wherein the term “about” refers to the indicated percentage +/−2.5%.

In some embodiments, the carrier gas is about 95% O₂ and about 5% N₂.

In some embodiments, the carrier gas is air.

In some embodiments, the liquid or emulsified reagent comprises an alkene.

In some embodiments, the liquid or emulsified reagent comprises an alkyne.

In some embodiments, the primary component of the liquid or emulsified reagent is methyl oleate.

In some embodiments, the liquid or emulsified reagent is derived from soy.

In some embodiments, the liquid or emulsified reagent is derived from palm oils.

In some embodiments, the liquid or emulsified reagent is derived from algal oils.

In some embodiments, waste water can be the reagent introduced into the reactor for the purpose of treating the water.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a diagram of the vertical cross-section of a multitubular reactor.

FIG. 2 is a diagram of the detail denoted by II in FIG. 1, on a larger scale.

FIG. 3 is a diagram of the cross-section along line III-III in FIG. 1.

DETAILED DESCRIPTION OF THE DISCLOSURE

The disclosure relates to the ozonolysis or ozone-related reactions which occur on the free surface of a film of a liquid or emulsified reagent or reagent mixture that is subject to the controlled amount of a gaseous reagent comprising ozone (O₃). The liquid or emulsified reagent or reagent mixture is the starting material which is reacted with ozone to yield oxidized product(s). The starting material is generally an alkene, alkyne, or any other compound that may be oxidized with ozone. The reaction products may be further reduced or oxidized to generate corresponding carbonyls, alcohols, and/or acids.

Performing ozone-based oxidation reactions in industrial-scale tubular falling film reactors (e.g., those originally designed for other processes, such as sulfonation) is advantageous for a variety of reasons. For example, tubular falling film sulfonation reactors operate by exposing relatively small volumes of liquid reagent(s) to relatively high volumes of reactive gaseous reagent(s) that have been diluted with an inert carrier gas or mixture thereof. Due to their continuous mode of operation, the reactors are efficient and exhibit reasonably high throughput rates per reactor tube, but do not allow for the accumulation of intermediates. Moreover, these reactors handle exothermic processes well because they include excellent heat dissipation features. The method described herein provides a safe and efficient means of performing ozonolysis reactions on an industrial scale by taking advantage of the aforementioned benefits of tubular falling film sulfonation reactors.

Examples of tubular falling film sulfonation reactors are described in GB 2,043,067 B, which is incorporated herein by reference. Tubular or multitubular co-current reactors are particularly useful due to their relatively low cost and mechanical simplicity. Such reactors can be adapted to use for ozonation reactions.

An additional safety advantage can be realized over traditional ozonolysis approaches if the reaction is carried out in water or as an emulsion with water. The flashpoint of the liquid reagent(s) can be eliminated or dramatically reduced in the presence of water, thereby minimizing the risk of fire in the event of an uncontrolled exotherm or explosion. Furthermore, the use of an emulsion allows for easier control of the liquid reagent in terms of concentration, distribution within the ozonolysis device tubes, and temperature.

As shown in FIGS. 1-3, the reactor 1 contains a set of parallel tubes 10 enclosed in a cylindrical housing, which is connected at one end to a gaseous reagent feeding chamber 70 and at the other end to a product collection chamber 40.

Gaseous ozone from an external source, such as a corona discharge or electrolysis driven ozone generating device, flows through conduit 12 into the feeding chamber 70 where it enters the tubes 10 and reacts with the liquid or emulsified reagent.

Reaction product(s) emerge from the tubes 10 into the product collection chamber 40, from which the reaction product(s) are removed via conduit 13 and collected in an external vessel.

A liquid coolant, such as water and/or glycol, flows into the reactor housing through conduit 20, around the tubes 10 and out of the reactor housing via conduit 21. Alternatively, the liquid coolant flows into the reactor housing through conduit 21 and out via conduit 20. The in conduit 20 and out conduit 21 direction of flow for the liquid coolant is preferred, however, because the exothermic reaction between ozone and the liquid or emulsified reagent(s) takes place preferentially at the portion of the tubes 10 that is closest to the feeding chamber 70. Numerous diaphrams 22, located inside the reactor housing and oriented perpendicular to the tubes 10, increase alter the path and increase the turbulence of the coolant flowing through the reactor housing. The coolant is separated from the gas feeding chamber and the product collection chamber by plates 23 and 24, respectively, which are oriented normal to, and positioned at the ends of the tubes 10.

Additional configurations for cooling the reactor that are not depicted in FIGS. 1-3 are also effective and may be employed. For example, the reactor housing interior may contain two separate cooling sections, one to cool the end of the tubes 10 that is connected to the feeding chamber 70 and one too cool the end of the tubes 10 that is connected to the product collection chamber 40, to enhance the overall cooling capacity.

A third tube plate 25 is positioned between the gas feeding chamber 70 and plate 23 such to define a feeding chamber 15 for the liquid or emulsified reagent(s). One or more conduits 16 are used to feed the liquid or emulsified reagent(s) into the feeding chamber 15, which also contains a device as shown in FIG. 2 for introducing the liquid or emulsified reagent(s) into one end of the tubes 10.

As shown in FIG. 2, each tube 10 has a cylindrical portion 30 with a slightly larger diameter than the remainder of the tube, which is connected to the tube by a frusto-conical section 31. The cylindrical portion 30 contains passages 38 for introducing the liquid or emulsified reagent(s) into the tube 10. The cylindrical portion 30 fits, with suitable clearance, in a cylindrical sleeve 33, the latter of which facilitates for the formation of liquid-tight seals between the cylindrical portion 30 and plates 23 and 25. The cylindrical sleeve 33 contains passages 36 for the liquid or emulsified reagent(s), of suitable size and circumferential distribution as not to generate head losses when allowing passage of the liquid or emulsified reagent(s) into the cylindrical portion 30.

The outer surface of a second sleeve 50 is in contact with the inner surface of the cylindrical portion 30, except for a central section, owing to the presence of a wide annular groove 51. The inner surface of the cylindrical portion 30 and groove 51 define an annular space for receiving the liquid or emulsified reagent(s) that enter the tube 10 from the passages 36 and 38, which open into groove 51. A seal groove 34 is positioned between the cylindrical sleeve 33 and the frusto-conical section 31. Suitable axial passages 52, shown only diagrammatically in FIG. 2, allow the liquid reagent to discharge into the tube interior from the annular space defined by groove 51. The sleeve 50 comprises a beveled or frusto-conical end with the same opening angle as the frusto-conical section 31.

Between one end of the second sleeve 50 and the frusto-conical section 31 there is an annular slot oriented according to the generatrices of a truncated cone, the width of this slot being defined by the gap space between sleeve 50 and the frusto-conical section 31. The gap space between sleeve 50 and the frusto-conical section 31 may be adjusted by a threaded crown 54 screwed into the end of the cylindrical portion 30 that is closest to the gas feeding chamber 70. It is thus possible, by screwing up or down the sleeve 50 in the cylindrical portion 30, to adjust the cross-section of the annular slot between the edge of the sleeve 50 and the frusto-conical section 31. The annular slot, being orientated according to the generatrices of a cone, favors the distribution of the liquid reagent in the form of a film entirely around the inner surface of the tube 10.

The inner diameter of sleeve 50 is suitably the same as the inner diameter of the tube 10 so that the gaseous reagent coming from the distribution chamber 70 may be brought to brush the free surface of the film 60 without resulting in a significant head loss.

Starting materials for the method described herein include any compound that may be oxidized by ozonolysis. Specific examples of starting materials for this process include hydroxycitronellene, methoxycitronellene, fatty acid methyl esters (FAME), triglycerides, fatty acids, fatty alcohols, fatty esters, diterpenes, sesquiterpenes, monoterpenes, allyl ethers, alpha olefins, and rosin acids.

In one embodiment, a tube reactor for ozonolysis includes a tube (see, e.g., 10 in FIG. 1) with a 5 to 30 mm internal diameter (e.g., 10 mm) and a length of 1 to 7 m (e.g., 1.7 m). The tube is constructed of a suitable material (e.g., stainless steel) and is connected to a gaseous reagent feeding chamber (see, e.g., 70 in FIG. 1) that allows gas to flow through the center of the tube and liquid to be flowed in a film on the wall of the tube through annular slots (e.g., as shown in FIG. 2; component II in FIG. 1). The tube is enclosed in a jacket (see, e.g., 1 in FIG. 1) for circulating liquid coolant around it (see, e.g., 10 in FIG. 1), with the end of the tube protruding through a liquid-sealed orifice (see, e.g., 24 in FIG. 1). A liquid/gas separation vessel is connected to the bottom of the reaction tube (see, e.g., 10 in FIG. 1). The excess gas flows into an ice condenser and then into an ozone destruction unit. The collected liquid product is pumped into sampling containers for analysis by a peristaltic pump.

In one embodiment, the gas inlet (see, e.g., 12 in FIG. 1) is connected to an ozone generator, and the liquid inlet is connected to a stirred feed tank equipped with a peristaltic pump. The liquid inlet pipe is also jacketed and cooled to control the temperature of the feed liquid or emulsified reagent.

In one embodiment, for emulsion preparation, water is combined with the organic reagent in a ratio (e.g., 5:1) ranging from stoichiometric (i.e., 1:1) to very dilute (e.g., 100:1) in the feed tank and stirred vigorously such that a homogenous emulsion is maintained. Deionized water is used for the emulsions.

In one embodiment, a mixture of O₂ and N₂ gas is used to feed the ozone generator and to comprise the ozone carrier gas for the ozonolysis reaction.

In one embodiment, conversions of starting materials are determined by gas chromatography (GC) and are calculated on the basis of the disappearance of starting material. Samples are prepared by extracting the organic components of the emulsion into a homogenous organic solvent phase. Analysis of the composition of the aforementioned organic phase is accomplished by gas chromatography.

In one embodiment, the ratio of water to organic reagent ranges from 1:1 to 100:1 (e.g., 5:1), the ozone concentration ranges from 2.5% to 10% (e.g., 5%), the gas flow rate ranges from 10 to 20 L/min (e.g., 15 L/min), the ozone mass flow rate ranges from 32.6 to 135 g/h (e.g., 65.9 g/h), the emulsion flow rate ranges from 1 to 5 kg/h (e.g., 2 kg/h), and the cooling temperature ranges from 0 to 20° C. (e.g., 10° C.), to yield starting material conversion percentages ranging from 13.70% to 52.63% (e.g., 26.76%).

In another embodiment, 1-6 pilot tube reactors (e.g., 3) can be connected in series, with gas and liquid being separated at the bottom of each tube. Tubes can be from 1-6 m in length (e.g., 1.7 m), and the tubes can range in diameter from 5-50 mm (e.g., the first 2 tubes being 25 mm in diameter and the 3^(rd) tube being 10 mm in diameter). The organic liquid feed can be flowed in a solution of reagent and nonanoic acid in ranges from 1:1 to 100:1 (e.g., 3:1) through the first tube to the second and third tube in series at rates ranging from 1-99 kg/hr (e.g., 4.2 kg/hr). The gas can be flowed co-currently at ozone concentration in ranges from 0.5% to 10% (e.g., 5.1%) from the 3^(rd) tube through the 2^(nd) to the 1^(st) tube at a flow rate from 10 to 1500 L/min (e.g., 150 L/min), and the cooling jacket temperature can be maintained between 0 and 50° C. (e.g., 15° C.) to yield conversion percentages between 93-100% (e.g., 97.6%).

EXAMPLES Example 1

Film Ozonolysis in a Monotubular Reactor

Ozonolysis Reactor Details

A pilot tube reactor was used for ozonolysis, including a tube with a 10 mm internal diameter and a length of 1.7 m (e.g., 10 in FIG. 1). The tube was constructed of 316 stainless steel and was connected to a gaseous reagent feeding chamber (e.g., 70 in FIG. 1) that allowed gas to be flowed through the center of the tube and liquid to be flowed in a film on the wall of the tube through annular slots (e.g., as shown in FIG. 2; component II in FIG. 1). The tube was enclosed in a steel jacket (e.g., 1 in FIG. 1) for circulating cooling fluid around the reaction tube (e.g., 10 in FIG. 1) with the end of the tube protruding through a liquid-sealed orifice (e.g., 24 in FIG. 1). A liquid/gas separation vessel was connected to the bottom of the reaction tube (e.g., 10 in FIG. 1). The excess gas flowed through to an ice condenser followed by an ozone destruction unit. The collected liquid product was pumped through a peristaltic pump to sampling containers for analysis.

The gas inlet (e.g., 12 in FIG. 1) was connected to an Ozonia Ozat CFS-2G ozone generator and the liquid inlet was connected to a stirred feed tank equipped with a peristaltic pump. The liquid inlet pipe was also jacketed and cooled to control the temperature of the feed liquid reagent.

Ozonolysis Reagent and Product Details

Methoxycitronellene was >99% pure and was obtained from reaction of methanol with dihydromyrcene. Fatty acid methyl esters (FAME) was obtained from multiple sources including soy, palm, and algal oils and consisted of 72-89% methyl oleate as the primary component.

When methoxycitronellene is reacted, the major product is methoxymelonal. When FAME is reacted, the major products are methyl azelaldehyde and nonanal.

For the emulsion preparation, water was combined with the organic reagent in a 5:1 ratio in the feed tank and stirred vigorously such that a homogenous emulsion was maintained. Deionized water was used for all of the emulsions.

A mixture of 95% O₂ and 5% N₂ gas was used to feed the ozone generator and to comprise the carrier gas for O₃ to the reaction.

Conversions of starting materials were determined by GC (Agilent 6890N) and were calculated based on the disappearance of the starting material on a gross adjusted basis. Samples were prepared by extracting the organic components of the emulsion into a homogenous ethyl acetate solvent phase and analyzing the composition of said organic phase by gas chromatography.

Example reaction conditions and product distributions are outlined in Tables 1 and 2. Reactions were performed at various O₃ concentrations and mass flow rates.

TABLE 1 Methoxycitronellene in a water-based emulsion was oxidized by ozonolysis at different ozone concentrations and flow rates to yield the starting material conversion percentages shown. Ratio of Water Gas O₃ Mass Emulsion Cooling Conversion of to Organic O₃ Conc Flowrate Flow Flow Temp Starting Material Sample Reagent (w/w) % L/min g/h kg/h ° C. % 1 5:1 2.5 15 32.6 2 10 13.70 2 5:1 2.5 15 32.6 2 10 15.79 3 5:1 5 15 65.9 2 10 26.76 4 5:1 5 15 65.9 2 10 24.71 5 5:1 10 15 135 2 10 48.89 6 5:1 10 15 135 2 10 52.63

TABLE 2 FAME (89% methyl oleate) in a water-based emulsion was oxidized by ozonolysis at different ozone concentrations and flow rates to yield the starting material conversion percentages shown. Ratio of Water Gas O₃ Mass Emulsion Cooling Conversion of to Organic O₃ Conc. Flowrate Flow Flow Temp Starting Material Sample Reagent (w/w) % L/min g/h kg/h ° C. % 1 5:1 4 15 52.5 2 25 42.4 2 5:1 4 15 52.5 2 25 38.8 3 5:1 6.4 15 85 2 25 46.5 4 5:1 6.4 15 85 2 25 50.4 5 5:1 9.5 15 128 2 25 50.9 6 5:1 9.5 15 128 2 25 51.3

Example 2

Ozonolysis Reactor 2 Details

A second arrangement of involving 3 pilot tube reactors connected in series was used. All 3 tubes were 1.7 m in length, with the first 2 tubes being 25 mm in diameter and the 3^(rd) tube being 10 mm in diameter. All tubes were equipped with a film distribution head, a cooling jacket, and a gas liquid separator at the bottom. The organic, liquid feed was flowed from the first tube through the second and third tube in series. The gas was flowed co-currently from the 3^(rd) tube through the 2^(nd) to the 1^(st) tube. The cooling jacket temperature was maintained at 15° C.

In one instance, this reactor was used to process a 75% mixture of vegetable fatty acid in nonanoic acid. The major components of the vegetable fatty acid were estimated as follows: 77.65% oleic acid, 11.64% linoleic acid, 1.98% stearic acid, 4.4% palmitic acid, 2.9% myristic acid. The O₃ was generated using pure O₂ and a generator composed of 2 Pinnacle Quadblocks in a custom cabinet. The results of this run are presented in Table 3.

TABLE 3 Ozonolysis of vegetable fatty acid in a film ozonolysis reactor. Sample 1 was taken at 10 minutes, Sample 2 at 15 minutes, and Sample 3 at 20 minutes. Conversion was based on disappearance of starting material on GC FID as compared to an internal standard. Ratio of O₃ Vegetable Fatty O₃ Gas Mass Liquid Cooling Conversion of Acid to Conc. Flowrate Flow Flow Temp Starting Material Sample Nonanoic Acid (w/w) % L/min g/h kg/h ° C. (oleic/linoleic) % 1 3:1 5.1 150 672 4.2 15 95.5/98.1 2 3:1 5.1 150 672 4.2 15 94.0/97.6 3 3:1 5.1 150 672 4.2 15 93.7/97.3

In another instance, this reactor was used to convert a 25% solution of dihydromyrcenol in water to hydroxymelonal. The results of this run are shown in Table 4.

TABLE 4 Ozonolysis of dihydromyrcenol, i.e., hydroxycitronellene, in the film ozonolysis reactor to generate hydroxymelonal. Samples were taken every 5 minutes. Conversion was based on GC FID results. Conversion Liquid of Starting Dihydromyrcenol O₃ % Gas flow O₃ Mass Flow Cooling Material Sample to Water Ratio (w/w) (L/min) Flow (g/hr) (ml/min) Temp ° C. (%) 1 3:1 7.8 80 555.8 80 5-15 99.8 2 3:1 7.8 80 555.8 80 5-15 99.5 3 3:1 7.8 80 555.8 80 5-15 98.5 4 3:1 7.8 80 555.8 80 5-15 97.2 5 3:1 7.8 80 555.8 80 5-15 98.3

Similar results were obtained for the conversion of β-Ionone to generate cyclocitral.

INCORPORATION BY REFERENCE

The entire disclosure of each of the patent documents and scientific articles referred to herein is incorporated by reference for all purposes.

EQUIVALENTS

The disclosure can be embodied in other specific forms without departing from the spirit or essential characteristics thereof. The foregoing embodiments are therefore to be considered in all respects illustrative rather than limiting on the disclosure described herein. Scope of the disclosure is thus indicated by the appended claims rather than by the foregoing description, and all changes that come within the meaning and range of equivalency of the claims are intended to be embraced therein. 

What is claimed is:
 1. A method of performing ozonolysis or ozone-based oxidation on a liquid or emulsified reagent using an industrial scale tubular falling film reactor with one or multiple tubes wherein the combined ozone and carrier gas flow is co-current, and wherein the ozonolysis occurs continuously without accumulation of large amounts of hazardous intermediates, and wherein the tubes are cooled by flow of a coolant; and wherein the gas flow rate is from 10 to 1500 L/min in each of said tube or tubes.
 2. The method of claim 1, wherein the diameter of the tube(s) is between 5 mm and 5 m, and the feeding pressure of the gaseous reagent is between 0.1 and 5 bar.
 3. The method of claim 1, wherein the diameter of the tube(s) is between 5 mm and 5 m, and wherein the feeding pressure of the gaseous reagent is between 0.1 and 0.5 bar.
 4. The method of claim 1, wherein the diameter of the tube(s) is between 5 mm and 30 mm, and the feeding pressure of the gaseous reagent is between 0.1 and 5 bar.
 5. The method of claim 1, wherein the diameter of the tube(s) is between 5 and 30 mm, and wherein the feeding pressure of the gaseous reagent is between 0.1 and 0.5 bar.
 6. The method of claim 1, wherein the diameter of the tube(s) is between 10 mm and 25 mm, and the feeding pressure of the gaseous reagent is between 0.1 and 5 bar.
 7. The method of claim 1, wherein the diameter of the tube(s) is between 10 and 25 mm, and wherein the feeding pressure of the gaseous reagent is between 0.1 and 0.5 bar.
 8. The method of claim 2, wherein the gas flow rate is about 150 L/min in each of said tube or tubes.
 9. The method of claim 3, wherein the gas flow rate is about 150 L/min in each of said tube or tubes.
 10. The method of claim 4, wherein the gas flow rate is about 150 L/min in each of said tube or tubes.
 11. The method of claim 5, wherein the gas flow rate is about 150 L/min in each of said tube or tubes.
 12. The method of claim 6, wherein the gas flow rate is about 150 L/min in each of said tube or tubes.
 13. The method of claim 7, wherein the gas flow rate is about 150 L/min in each of said tube or tubes.
 14. The method of claim 1, wherein the gas flow rate is about 150 L/min in each of said tube or tubes.
 15. The method of claim 1, wherein the coolant maintains the temperature between 0° C. and 50° C.
 16. A method of performing ozonolysis or ozone-based oxidation on a liquid or emulsified reagent with a gaseous reagent comprising ozone and one or more carrier gases, the method comprising: (a) feeding the liquid or emulsified reagent from a common liquid or emulsified reagent feeding chamber that is maintained completely full through annular slots and into a plurality of parallel and substantially identical tubes, as to form a liquid or emulsified reagent film on the internal surface of each tube; (b) feeding the gaseous reagent through the annular slots and into the tubes from a gaseous reagent feeding chamber, the feeding pressure of the gaseous reagent being substantially the same as the pressure loss from the gaseous reagent flow through the tubes containing the liquid or emulsified reagent film, but less than the feeding pressure of the liquid or emulsified reagent; and (c) cooling the tubes by flowing a liquid coolant through a housing surrounding the tubes; and wherein the gas flow rate in each of said parallel tubes is from 10 to 1500 L/min.
 17. The method of claim 16, further comprising (d) collecting reaction product(s) and gaseous reagent exhaust in one or more product containers connected to the end of the tubes opposite that connected to the annular slots.
 18. The method of claim 1, wherein the length of the tubes is greater than 1 m and less than 20 m.
 19. The method of claim 16, wherein the length of the tubes is greater than 1 m and less than 20 m.
 20. The method of claim 1, wherein the liquid or emulsified reagent comprises hydroxycitronellene.
 21. The method of claim 1, wherein the liquid or emulsified reagent comprises methoxycitronellene.
 22. The method of claim 21, wherein the product is methoxymelonal.
 23. The method of claim 16, wherein the gas flow rate in each of said parallel tubes is about 150 L/min. 